Method for reducing organic fluoride levels in hydrocarbons

ABSTRACT

A system and/or process for decreasing the level of at least one organic fluoride present in a hydrocarbon mixture by first passing the hydrocarbon mixture to an eductor and educting into the hydrocarbon mixture a catalyst comprising a volatility reducing additive and hydrofluoric acid to produce a hydrocarbon-catalyst mixture, permitting the hydrocarbon-catalyst mixture to undergo a phase separation to produce a hydrocarbon phase having a lower concentration of at least one organic fluoride than the hydrocarbon mixture and to produce a catalyst phase, and withdrawing at least a portion of the hydrocarbon phase to thereby form a hydrocarbon product stream, are disclosed. In an alternative embodiment, a system and/or process for controlling the concentration of at least one organic fluoride and/or the RON of the hydrocarbon mixture by adjusting the amount of volatility reducing additive present in the catalyst are disclosed.

This application is a division of application Ser. No. 09/238,244, filedJan. 27, 1999, now U.S. Pat. No. 6,114,593.

The present invention relates to a method and/or system for reducing theconcentration of organic fluorides present in a hydrocarbon mixture.More particularly, the invention relates to a method and/or system forreducing the concentration of organic fluorides present in an alkylationreactor effluent.

BACKGROUND OF THE INVENTION

The use of catalytic alkylation processes to produce branchedhydrocarbons having properties that are suitable for use as gasolineblending components is well known in the art. Generally, the alkylationof olefins by saturated hydrocarbons, such as isoparaffins, isaccomplished by contacting the reactants with an acid catalyst to form areaction mixture, settling the mixture to separate the catalyst from thehydrocarbons and further separating the alkylation reactor effluent, forexample, by fractionation, to recover the separate product streams.Normally, the alkylation reactor effluent of the alkylation processcontains hydrocarbons having five to ten carbon atoms per molecule,preferably seven to nine carbons atoms per molecule. In order to havethe highest quality gasoline blending stock, it is preferred for thealkylate hydrocarbons formed in the alkylation process to be highlybranched and contain seven to nine carbon atoms per molecule.

Recent efforts to improve conventional hydrogen fluoride catalyzedalkylation processes have resulted in the development of new catalystcompositions that contain hydrogen fluoride and a volatility reducingadditive. These new catalyst compositions have been found to be quiteeffective as an alkylation catalyst and to provide many other favorablebenefits. However, it has also been found that in the alkylation processthat uses the catalyst mixture containing hydrogen fluoride and suchadditive there is an increase in the production of undesirable organicfluorides. In fact, as the concentration of hydrogen fluoride in the newcatalyst composition becomes more dilute, the amount of organicfluorides produced in the alkylation process increases. Organicfluorides produced can include, but are not limited to, organicfluorides having in the range of from about 3 to about 14 carbon atomsper molecule. Typical organic fluorides produced can include, but arenot limited to, 2-fluoropropane, 2-fluorobutane,2-fluoro-2-methylpropane, 2-fluoropentane, 2-fluoro-2-methylbutane,2-fluoro-3-methylbutane, methylfluorobutane isomers, 2-fluorohexane,3-fluorohexane, methylfluoropentanes, dimethylfluorobutanes,fluoroheptanes, fluoromethylhexanes, dimethylfluoropentanes,fluorooctanes, fluoromethylheptanes, dimethylfluorohexanes,fluorotrimethylpentanes fluorononanes, fluoromethyloctanes,dimethylfluoroheptanes, fluorotrimethylhexanes.

In many instances, it is not desirable for the product streams to havean excessively high concentration of organic fluorides.

Therefore, development of an efficient process for reducing the level oforganic fluorides present in a hydrocarbon mixture would be asignificant contribution to the art.

BRIEF SUMMARY OF THE INVENTION

It is, thus, an object of the present invention to provide an improvedprocess for reducing the level of at least one organic fluoride in ahydrocarbon mixture which is economical and efficient.

A further object of the present invention is to provide an improvedsystem to be used in reducing the level of at least one organic fluoridein a hydrocarbon mixture which is economical in construction andreliable and efficient in operation.

A yet further object of the present invention is to provide an improvedsystem to be used in reducing the level of at least one organic fluoridein a hydrocarbon mixture which includes means for controlling the levelof at least one organic fluoride present in the hydrocarbon mixtureand/or for controlling the research octane of the hydrocarbon mixture.

According to a first embodiment of the present invention, a method fordecreasing the level of at least one organic fluoride present in ahydrocarbon mixture is provided. The method of the first embodimentcomprises the steps of:

passing the hydrocarbon mixture to an eductor;

educting into the hydrocarbon mixture a catalyst comprising a volatilityreducing additive and hydrofluoric acid to thereby form ahydrocarbon-catalyst mixture;

permitting the hydrocarbon-catalyst mixture to undergo a phaseseparation to thereby produce a hydrocarbon phase having a lowerconcentration of at least one organic fluoride than the hydrocarbonmixture and to thereby produce a catalyst phase;

withdrawing at least a portion of the catalyst phase for use as thecatalyst; and

withdrawing at least a portion of the hydrocarbon phase to form ahydrocarbon product stream.

According to a second embodiment of the present invention, a process foralkylating at least a portion of a hydrocarbon feedstock comprisingolefins and isoparaffins is provided. The process of the secondembodiment comprises the steps of:

introducing the hydrocarbon feedstock into an alkylation reaction zone;

contacting the hydrocarbon feedstock with a first catalyst comprising avolatility reducing additive and hydrofluoric acid in the alkylationreaction zone to thereby produce alkylation of at least a portion of theolefins and isoparaffins in the form of an alkylation reaction effluent;

passing the thus-produced alkylation reaction effluent from thealkylation reaction zone to a first settling zone and permitting a phaseseparation to occur so as to produce a first catalyst phase and toproduce a first hydrocarbon phase having a concentration of at least oneorganic fluoride in the range of from about 150 ppmw to about 10,000ppmw, based on the total weight of the first hydrocarbon phase, andhaving a research octane in the range of from about 85 to about 98; and

contacting at least a portion of the first hydrocarbon phase with asecond catalyst comprising a volatility reducing additive andhydrofluoric acid to thereby produce a hydrocarbon product stream havinga lower concentration of at least one organic fluoride than the firsthydrocarbon phase.

According to a third embodiment of the present invention, a system orapparatus is provided comprising:

an alkylation reactor;

a first settler, having an upper portion, an intermediate portion and alower portion;

an eductor;

a second settler, having an upper portion, an intermediate portion and alower portion;

first conduit means operably related to the alkylation reactor forintroducing a hydrocarbon feedstock comprising olefins and isoparaffinsinto the alkylation reactor;

second conduit means operably related to the alkylation reactor forintroducing a first catalyst comprising a volatility reducing additiveand hydrofluoric acid into the alkylation reactor;

third conduit means operably related to the alkylation reactor andoperably related to the first settler for withdrawing an alkylationreaction effluent from the alkylation reactor and for introducing thealkylation reaction effluent into the intermediate portion of the firstsettler, the upper portion of the first settler being operable forcontaining a first hydrocarbon phase separated from the alkylationreaction effluent and the lower portion of the first settler beingoperable for containing a first catalyst phase separated from thealkylation reaction effluent;

fourth conduit means operably related to the first settler and operablyrelated to the eductor for withdrawing at least a portion of the firsthydrocarbon phase from the upper portion of the first settler and forintroducing the at least a portion of the first hydrocarbon phase intothe eductor;

fifth conduit means, operably related to the second settler and operablyrelated to the eductor for withdrawing at least a portion of a secondcatalyst phase comprising a volatility reducing additive andhydrofluoric acid from the lower portion of the second settler and forintroducing the at least a portion of the second catalyst phase into theeductor for mixing with the at least a portion of the first hydrocarbonphase to thereby produce a hydrocarbon-catalyst mixture;

sixth conduit means operably related to the eductor and operably relatedto the second settler for withdrawing the hydrocarbon-catalyst mixturefrom the eductor and for introducing the hydrocarbon-catalyst mixtureinto the intermediate portion of the second settler, the upper portionof the second settler being operable for containing a second hydrocarbonphase separated from the hydrocarbon-catalyst mixture and the lowerportion of the second settler being operable for containing the secondcatalyst phase separated from the hydrocarbon-catalyst mixture; and

seventh conduit means operably related to the second settler forwithdrawing at least a portion of the second hydrocarbon phase from thesecond settler to thereby form a hydrocarbon product stream.

Other objects and advantages will become apparent from the detaileddescription and the appended claims.

BRIEF DESCRIPTION OF THE DRAWING

The FIGURE is a schematic flow diagram presenting an embodiment of thepresent invention.

DETAILED DESCRIPTION OF THE INVENTION

According to the first embodiment of the present invention, thehydrocarbon mixture can comprise paraffins and/or olefins, wherein eachof these hydrocarbons contains at least 3 carbon atoms per molecule. Thehydrocarbon mixture further comprises at least one organic fluoride inthe range of from about 150 ppmw to about 10,000 ppmw, based on thetotal weight of the hydrocarbon mixture. More typically, theconcentration of the at least one organic fluoride is in the range offrom about 200 ppmw to about 1,000 ppmw; and most typically from 250ppmw to 500 ppmw, based on the total weight of the hydrocarbon mixture.

The research octane number (RON) of the hydrocarbon mixture is typicallyin the range of from about 85 to about 98, more typically from about 87to about 96; and most typically from 89 to 94. RON, as used herein, isdefined as the octane number of a hydrocarbon stream as determined usingthe ASTM D2699-97 method.

The hydrocarbon mixture is most suitably an alkylation reaction productproduced from the alkylation of olefins having at least 3 carbon atomsper molecule with isoparaffins having at least 4 carbon atoms permolecule.

The hydrocarbon mixture can be contacted with a catalyst comprising avolatility reducing additive and hydrofluoric acid by any suitablemanner, including mixing and blending. The volatility reducing additivecan be any compound effective in reducing the volatility of a mixtureresulting from the addition of the volatility reducing additive tohydrofluoric acid. More particularly, the volatility reducing additivecan be a compound selected from the group consisting of sulfone,ammonia, methylamines, ethylamines, propylamines, butylamines,pentylamines, pyridine, alkylpyridines, picoline, melamine,hexamethylene-tetramine and the like.

The sulfones suitable for use in this invention are the sulfones of thegeneral formula

R—SO₂—R¹

wherein R and R¹ are monovalent hydrocarbon alkyl or aryl substituents,each containing from 1 to 8 carbon atoms, and wherein R and R¹ can bethe same or different. Examples of suitable sulfones include, but arenot limited to, dimethylsulfone, di-n-propylsulfone, diphenylsulfone,ethylmethylsulfone and alicyclic sulfones wherein the SO₂ group isbonded to a hydrocarbon ring. In such a case, R and R¹ are formingtogether a branched or unbranched hydrocarbon divalent moiety preferablycontaining from 3 to 12 carbon atoms. Among the latter,tetramethylenesulfone or sulfolane, 3-methylsulfolane and2,4-dimethylsulfolane are more particularly suitable since they offerthe advantage of being liquid at process operating conditions of concernherein. These sulfones may also have substituents, particularly one ormore halogen atoms, such as for example, chloromethylethylsulfone. Thesesulfones may advantageously be used in the form of mixtures of any twoor more thereof. The most preferred volatility reducing additive issulfone.

It is preferred to contact the hydrocarbon mixture with the catalyst bymixing in an eductor which can also be referred to as an ejector,siphon, exhauster or jet pump. As used herein, the operation andapparatus of the eductor are such to allow a pumping fluid to enterthrough a nozzle, pass through a venturi nozzle, and discharge through adischarge opening. As the pumping fluid passes into the venturi nozzle,it develops a suction that causes fluid in a suction chamber to beentrained with the pumping fluid stream and to be delivered through thedischarge opening.

The hydrocarbon mixture is passed to the pumping fluid inlet of aneductor wherein the catalyst is educted into the hydrocarbon mixture tothereby produce a hydrocarbon-catalyst mixture. The hydrocarbon-catalystmixture is then permitted to undergo a phase separation in a settlervessel thereby producing a hydrocarbon phase and a catalyst phase. Thehydrocarbon phase has a lower concentration of at least one organicfluoride than the hydrocarbon mixture. More particularly, theconcentration of at least one organic fluoride in the hydrocarbon phaseis preferably in the range of from about 0 ppmw to about 1,000 ppmw;more preferably from about 0 ppmw to about 100 ppmw; and most preferablyfrom 0 ppmw to 50 ppmw, based on the total weight of the hydrocarbonphase.

The RON of the hydrocarbon phase is preferably in the range of fromabout 85 to about 98, more preferably from about 87 to about 96, andmost preferably from 89 to 94.

In addition, at least a portion of the catalyst phase can be used as thecatalyst and at least a portion of the hydrocarbon phase is withdrawnfrom the process to form a hydrocarbon product stream.

The volatility reducing additive concentration of the catalyst is suchas to provide a hydrocarbon phase having a lower concentration of atleast one organic fluoride than the hydrocarbon mixture.

More particularly, the volatility reducing additive is present in thecatalyst in an amount in the range of from exceeding about 0 weightpercent to about 50 weight percent; preferably from about 5 weightpercent to about 35 weight percent; and most preferably from 10 weightpercent to 25 weight percent, based on the total weight of the catalyst.

The concentration of the volatility reducing additive in the catalystcan be varied so as to adjust and/or control the concentration of atleast one organic fluoride in the hydrocarbon product stream and/or toadjust and/or control the RON of the hydrocarbon product stream.

More particularly, the concentration of the volatility reducing additivein the catalyst can be varied by replacing at least a portion of thecatalyst phase with a makeup catalyst comprising a compound selectedfrom the group consisting of the volatility reducing additive,hydrofluoric acid, and mixtures thereof.

The amount of volatility reducing additive can be adjusted such that theRON of the hydrocarbon product stream is controlled to a level in therange of from about 85 to about 98; preferably from about 87 to about96; and most preferably from 89 to 94; and/or such that theconcentration of the at least one organic fluoride present in thehydrocarbon product stream is controlled to a level in the range of fromabout 0 percent to about 65 percent; preferably from about 0 percent toabout 50 percent; and most preferably from 0 percent to 25 percent ofthe concentration of the at least one organic fluoride of thehydrocarbon mixture.

According to the second embodiment of the present invention, thehydrocarbon feedstock can comprise iso-paraffins having at least 4carbon atoms per molecule and olefins having at least 3 carbon atoms permolecule. Preferably, the iso-paraffins have in the range of from 4 to 5carbon atoms per molecule and the olefins have in the range of from 3 to4 carbon atoms per molecule.

The olefins contained in the hydrocarbon feedstock can be alkylated withthe iso-paraffins by contacting the hydrocarbon feedstock, by anysuitable manner in an alkylation reaction zone, with a first catalystcomprising hydrofluoric acid and a volatility reducing additive (asdescribed above) to thereby produce alkylation of at least a portion ofthe olefins and iso-paraffins in the form of an alkylation reactioneffluent comprising alkylate, unreacted iso-paraffins, the firstcatalyst, and, in runaway type situations, unreacted olefins.

The alkylation reaction effluent can be passed from the alkylationreaction zone to a first settling zone wherein a phase separationoccurs. The phase separation produces a first hydrocarbon phase having aconcentration of at least one organic fluoride in the range of fromabout 150 ppmw to about 10,000 ppmw; more particularly from about 200ppmw to about 1,000 ppmw; and most particularly from 250 ppmw to 500ppmw, based on the total weight of the first hydrocarbon phase; and thefirst hydrocarbon phase has a RON in the range of from about 85 to about98; more particularly from about 87 to about 96; and most particularlyfrom 89 to 94. The first hydrocarbon phase can comprise alkylate,unreacted iso-paraffins, and unreacted olefins.

The phase separation in the first settling zone also produces a firstcatalyst phase which can be used, at least in part, as the firstcatalyst. At least a portion of the first hydrocarbon phase can becontacted with a second catalyst comprising a volatility reducingadditive and hydrofluoric acid by any suitable manner, including mixingand blending to thereby produce a hydrocarbon product stream. It ispreferred to contact at least a portion of the first hydrocarbon phasewith the second catalyst by mixing in an eductor.

At least a portion of the first hydrocarbon phase is passed to aneductor wherein the second catalyst is educted into at least a portionof the first hydrocarbon phase to thereby form a hydrocarbon-catalystmixture. The hydrocarbon-catalyst mixture is then passed to a secondsettling zone wherein a phase separation occurs thereby producing asecond hydrocarbon phase and a second catalyst phase. The secondhydrocarbon phase has a lower concentration of at least one organicfluoride than the first hydrocarbon phase. More particularly, theconcentration of at least one organic fluoride in the second hydrocarbonphase is preferably in the range of from about 0 ppmw to about 1,000ppmw; more preferably from about 0 ppmw to about 100 ppmw; and mostpreferably from 0 ppmw to 50 ppmw, based on the total weight of thesecond hydrocarbon phase.

The second hydrocarbon phase has a RON in the range of from about 85 toabout 98; preferably from about 87 to about 96; and most preferably from89 to 94.

In addition, at least a portion of the second catalyst phase can be usedas the second catalyst and at least a portion of the second hydrocarbonphase is withdrawn from the process to form a hydrocarbon productstream.

The volatility reducing additive concentration of the second catalyst issuch as to provide the second hydrocarbon phase having a lowerconcentration of at least one organic fluoride than the firsthydrocarbon phase. For best results in decreasing the concentration ofat least one organic fluoride in the first hydrocarbon phase, theconcentration of volatility reducing additive in the second catalyst isless than the concentration of volatility reducing additive in the firstcatalyst. More particularly, the volatility reducing additive is presentin the second catalyst in an amount in the range of from exceeding about0 weight percent to about 50 weight percent; preferably from about 5weight percent to about 35 weight percent; and most preferably from 10weight percent to 25 weight percent based on the total weight of thesecond catalyst.

The amount of volatility reducing additive present in the secondcatalyst can be varied in order to control at least one processingvariable, such as, but not limited to, the concentration of at least oneorganic fluoride of the hydrocarbon product stream and/or the RON of thehydrocarbon product stream.

Where the processing variable is the concentration of at least oneorganic fluoride, the concentration of the volatility reducing additivepresent in the second catalyst can be decreased responsive to anincrease in the concentration of at least one organic fluoride of thehydrocarbon product stream above a desired concentration of at least oneorganic fluoride of the hydrocarbon product stream to thereby decreasethe concentration of at least one organic fluoride of the hydrocarbonproduct stream. Alternately, the concentration of the volatilityreducing additive present in the second catalyst can be increasedresponsive to a decrease in the concentration of at least one organicfluoride in the hydrocarbon product stream below the desiredconcentration to thereby increase the concentration of at least oneorganic fluoride of the hydrocarbon product stream.

Where the processing variable is RON, the concentration of thevolatility reducing additive present in the second catalyst can bedecreased responsive to an increase in the RON of the hydrocarbonproduct stream above a desired RON of the hydrocarbon product stream tothereby decrease the RON of the hydrocarbon product stream. Alternately,the concentration of the volatility reducing additive present in thesecond catalyst can be increased responsive to a decrease in the RON ofthe hydrocarbon product stream below the desired RON to thereby increasethe RON of the hydrocarbon product stream.

One skilled in the art can establish the concentration of the volatilityreducing additive present in the second catalyst at a level whichmaximizes the RON of the hydrocarbon product stream, or, which minimizesthe concentration of at least one organic fluoride of the hydrocarbonproduct stream, or, which reaches a desired balance between the RON andthe concentration of at least one organic fluoride of the hydrocarbonproduct stream.

The desired concentration of at least one organic fluoride of thehydrocarbon product stream is preferably in the range of from about 0percent to about 65 percent; more preferably from about 0 percent toabout 50 percent; and most preferably from 0 percent to 25 percent ofthe concentration of at least one organic fluoride of the firsthydrocarbon phase.

The desired RON of the hydrocarbon product stream is preferably in therange of from about 85 to about 98; more preferably from about 87 toabout 96; and most preferably from 89 to 94.

For best results in decreasing the concentration of at least one organicfluoride in the first hydrocarbon phase, the ratio by weight ofiso-butane to alkylate in the first hydrocarbon phase is in the range offrom about 1:1 to about 8:1, preferably from about 1.5:1 to about 6:1;and most preferably from 2:1 to 5:1.

According to the third embodiment of the present invention, the systemof the present invention will be described with reference to thedrawing.

Referring to the FIGURE therein is illustrated the inventive system orapparatus 10 including an alkylation reactor 100 having an inside wall102 which defines an alkylation reaction zone. The alkylation reactor100 is operably related by connection in fluid flow communication to aconduit 104 providing first conduit means for introducing a hydrocarbonfeedstock into the alkylation reaction zone. The alkylation reactor 100is also operably related by connection in fluid flow communication to aconduit 106 providing second conduit means for introducing a firstcatalyst comprising a volatility reducing additive, as described above,and hydrofluoric acid into the alkylation reaction zone. The alkylationreactor 100 provides means for alkylating at least a portion of thehydrocarbon feedstock to thereby produce an alkylation reactioneffluent.

The alkylation reactor 100 is operably related by connection in fluidflow communication to a conduit 108 providing third conduit means forremoving the alkylation reaction effluent from alkylation reactor 100and for introducing the alkylation reaction effluent into anintermediate portion 109 of a first settler 110. First settler 110 alsohas an inside wall 112 which defines a first settling zone, having anupper portion 114, intermediate portion 109 and a lower portion 116, forallowing a phase separation of the alkylation reaction effluent. Theupper portion 114 of first settler 110 is operable for containing afirst hydrocarbon phase separated from the alkylation reaction effluentand the lower portion 116 of first settler 110 is operable forcontaining a first catalyst phase separated from the alkylation reactioneffluent.

The lower portion 116 of first settler 110 is operably related byconnection in fluid flow communication, via conduit 106, with alkylationreactor 100 for returning the first catalyst phase to alkylation reactor100 for use as the first catalyst.

The upper portion 114 of first settler 110 is operably related byconnection in fluid flow communication to a conduit 118 providing fourthconduit means for withdrawing at least a portion of the firsthydrocarbon phase from upper portion 114 of first settler 110 and forintroducing at least a portion of the first hydrocarbon phase into aneductor 120. Eductor 120 is operably related by connection in fluid flowcommunication via conduit 122 with a second settler 124 having an insidewall 126 which defines a second settling zone having an upper portion128, an intermediate portion 129 and a lower portion 130. Conduit 122provides fifth conduit means for withdrawing at least a portion of asecond catalyst phase comprising a volatility reducing additive andhydrofluoric acid from the lower portion 130 of second settler 124 andfor introducing at least a portion of the second catalyst phase intoeductor 120 for mixing with at least a portion of the first hydrocarbonphase introduced via conduit 118 into eductor 120 to thereby produce ahydrocarbon-catalyst mixture.

Eductor 120 is operably related by connection in fluid flowcommunication to a conduit 132 which provides sixth conduit means forwithdrawing the hydrocarbon-catalyst mixture from eductor 120 and forintroducing the hydrocarbon-catalyst mixture into the intermediateportion 129 of second settler 124. The upper portion 128 of secondsettler 124 is operable for containing a second hydrocarbon phaseseparated from the hydrocarbon-catalyst mixture and the lower portion130 of the second settler 124 is operable for containing the secondcatalyst phase separated from the hydrocarbon-catalyst mixture.

Upper portion 128 of second settler 124 is operably related byconnection in fluid flow communication to a conduit 134 which providesseventh conduit means for withdrawing at least a portion of the secondhydrocarbon phase from upper portion 128 of second settler 124 tothereby form a hydrocarbon product stream.

In addition, the inventive system or apparatus 10 can include a controlsystem operably related to second settler 124 which provides controlmeans for varying the concentration of the volatility reducing additivepresent in the second catalyst phase in order to control at least oneprocessing variable of the hydrocarbon product stream.

Dash lines, which designate signal lines in the drawings, are electricalor pneumatic in this preferred embodiment. However, the invention isalso applicable to mechanical, hydraulic, or other signal means fortransmitting information. In almost all control systems some combinationof these types of signals will be used. However, the use of any othertype of signal transmission, compatible with the process and equipmentin use, is within the scope of the invention.

A digital computer is used in the preferred embodiment of this inventionto calculate the required control signal based on measured processparameters as well as set points supplied to the computer. Any computercontrol system having software that allows operation in a real timeenvironment for reading values of external variables and transmittingsignals is suitable for use in this invention.

Signal lines are also utilized to represent the results of calculationscarried out in a digital computer and the term “signal” is utilized torefer to such results. Thus, the term signal is used not only to referto electrical currents or pneumatic pressures but is also used to referto binary representations of a calculated or measured value.

The controllers shown may utilize the various modes of control such asproportional, proportional-integral, proportional-derivative, orproportional-integral-derivative. In this preferred embodiment,proportional-integral-derivative controllers are utilized but anycontroller capable of accepting two input signals and producing a scaledoutput signal, representative of a comparison of the two input signals,is within the scope of the invention.

The scaling of an output signal by a controller is well known in controlsystem art. Essentially, the output of a controller may be scaled torepresent any desired factor or variable. An example of this is where adesired flow rate and an actual flow rate are compared by a controller.The output could be a signal representative of a desired change in theflow rate of some liquid necessary to make the desired and actual flowsequal. On the other hand, the same output signal could be scaled torepresent a percentage or could be scaled to represent a temperaturechange required to make the desired and actual flows equal. If thecontroller output can range from 0 to 10 volts, which is typical, thenthe output signal could be scaled so that an output signal having avoltage level of 5.0 volts corresponds to 50 percent of some specifiedflow rate.

The various transducing means used to measure parameters whichcharacterize the process and the various signals generated thereby maytake a variety of forms or formats. For example, the control elements ofthe system can be implemented using electrical analog, digitalelectronic, pneumatic, hydraulic, mechanical or other similar types ofequipment or combinations of one or more such equipment types. While thepresently preferred embodiment of the invention preferably utilizes acombination of pneumatic final control elements in conjunction withelectrical analog signal handling and translation apparatus, theapparatus and method of the invention can be implemented using a varietyof specific equipment available to and understood by those skilled inthe process control art.

Likewise, the format of the various signals can be modifiedsubstantially in order to accommodate signal format requirements of theparticular installation, safety factors, the physical characteristics ofthe measuring or control instruments and other similar factors. Forexample, a raw flow measurement signal produced by a differentialpressure orifice flow meter would ordinarily exhibit a generallyproportional relationship to the square of the actual flow rate. Othermeasuring instruments might produce a signal which is proportional tothe measured parameter, and still other transducing means may produce asignal which bears a more complicated, but known, relationship to themeasured parameter. Regardless of the signal format or the exactrelationship of the signal to the parameter which it represents, eachsignal representative of a measured process parameter or representativeof a desired process value will bear a relationship to the measuredparameter or desired value which permits designation of a specificmeasured or desired value by a specific signal value. A signal which isrepresentative of a process measurement or desired process value istherefore one from which the information regarding the measured ordesired value can be readily retrieved regardless of the exactmathematical relationship between the signal units and the measured ordesired process units.

Referring again to the FIGURE, the control system comprises a conduit136 which is operably related by connection in fluid flow communicationto lower portion 130 of second settler 124. Conduit 136 provides aneighth conduit means for introducing a hydrofluoric acid stream into thesecond catalyst phase, and a conduit 138 which is operably related byconnection in fluid flow communication to lower portion 130 of secondsettler 124 provides a ninth conduit means for introducing a volatilityreducing additive stream into the second catalyst phase. Thehydrofluoric acid stream in conduit 136 can be combined with thevolatility reducing additive stream in conduit 138 prior to introductioninto the second catalyst phase contained in lower portion 130 of secondsettler 124. A conduit 140 is operably related by connection in fluidflow communication to lower portion 130 of second settler 124 andprovides tenth conduit means for withdrawing a purge stream from thesecond catalyst phase.

Conduit 136 is operably related to a first control valve 142 interposedtherein which provides first control valve means for adjusting the flowrate of the hydrofluoric acid stream through conduit 136. Conduit 138 isoperably related to a second control valve 144 interposed therein whichprovides second control valve means for adjusting the flow rate of thevolatility reducing additive stream through conduit 138. Conduit 140 isoperably related to a third control valve 146 interposed therein whichprovides third control valve means for adjusting the flow rate of thepurge stream through conduit 140.

Operably associated with each of the conduits 136, 138 and 140 is arespective flow transducer 148, 150 and 152, each of which produces arespective flow signal 154, 156 and 158 which is representative of thevolume flow rate of the material carried through the conduits with whichit is associated. Flow transducers 148, 150 and 152 can comprise flowmeasuring devices, such as orifice plates, located within conduits 136,138 and 140, respectively, for measuring the volume flow rates.

Analyzer 160, which is preferably a chromatograph, provides means forestablishing a processing variable signal 162 representative of theactual value of at least one processing variable of the hydrocarbonproduct stream. Analyzer 160 is preferably adapted to take a sample offresh hydrocarbon product stream from conduit 134 and to deliver, inresponse to the analysis of the hydrocarbon product stream, processingvariable signal 162 which is representative of the actual value of theat least one processing variable of the hydrocarbon product stream.Analyzer 160 can include off-line analysis of the sample of thehydrocarbon product stream.

A computer calculation block 164, preferably associated with adistributed control system, receives as inputs thereto the flow ratesignals 154, 156 and 158, processing variable signal 162 and an operatorentered signal 166 which is representative of the desired value for theat least one processing variable of the hydrocarbon product streamflowing in conduit 134. Computer calculation block 164 establishesoutput signals 168, 170 and 172, each responsive to signals 154, 156 and158 and to the difference between signals 162 and 166. Signals 168, 170and 172 are scaled to be representative of the flow rates of thehydrofluoric acid stream in conduit 136, the volatility reducingadditive stream in conduit 138 and the purge stream in conduit 140,respectively, required to maintain the actual value of the at least oneprocessing variable represented by signal 162 substantially equal to thedesired value of the at least one processing variable represented bysignal 166.

Signal 168 is provided as a set point input to flow controller 174. Alsoprovided as a processing variable input to flow controller 174 is flowrate signal 154 which is representative of the actual flow rate ofhydrofluoric acid in conduit 136. Flow controller 174 provides an outputsignal 176 which is responsive to the difference between signals 168 and154. Signal 176 is scaled to be representative of the position of firstcontrol valve 142 required to maintain the flow rate represented bysignal 154 substantially equal to the flow rate represented by signal168.

Signal 170 is provided as a set point input to flow controller 178. Alsoprovided as a processing variable input to flow controller 178 is flowrate signal 156 which is representative of the actual flow rate of thevolatility reducing additive in conduit 138. Flow controller 178provides an output signal 180 which is responsive to the differencebetween signals 170 and 156. Signal 180 is scaled to be representativeof the position of second control valve 144 required to maintain theflow rate represented by signal 156 substantially equal to the flow raterepresented by signal 170.

Signal 172 is provided as a set point input to flow controller 182. Alsoprovided as a processing variable input to flow controller 182 is flowrate signal 158 which is representative of the actual flow rate of thepurge stream in conduit 140. Flow controller 182 provides an outputsignal 184 which is responsive to the difference between signals 172 and158. Signal 184 is scaled to be representative of the position of thirdcontrol valve 146 required to maintain the flow rate represented bysignal 158 substantially equal to the flow rate represented by signal172.

The following example is provided to further illustrate this inventionand is not to be considered as unduly limiting the scope of thisinvention.

EXAMPLE

This example illustrates the use of catalysts comprising hydrofluoricacid and a volatility reducing additive in the reduction of organicfluoride levels in a hydrocarbon mixture.

A reactor was constructed to enable the steady-state evaluation ofHF/sulfolane catalysts comprising varying levels of hydrofluoric acidand sulfolane. The reactor was a section of monel schedule 40 pipe 2feet in length and 1 inch in diameter connected at one end to a monelsight gauge via ¼″ monel tubing, and connected at the other end to afeed introduction nozzle, having a 0.01 inch diameter orifice, via ⅛″monel tubing.

The catalyst was circulated through the reactor and monel sight gauge ata flow rate in the range of from about 50 mL/min to about 100 mL/min.The catalyst composition was varied for each run, as shown in the Table.A hydrocarbon feed comprising a 2/1 by weight mixture ofisobutane/alkylate was blended into a feed cylinder. The alkylate wasobtained from an alkylation unit of a refinery. For each run, thehydrocarbon feed was pumped through the feed introduction nozzle intothe reactor at a rate of about 300 mL/hour. The reactor effluent flowedinto the monel sight gauge wherein the hydrocarbon product and anycatalyst carryover were separated.

The hydrocarbon product was drawn off into a suitable sample cylinder,passed over alumina at an ambient temperature (to adsorb free HF),collected, and analyzed by standard gas chromatography using a GC sampleinjection valve so that no light materials were lost. Test data resultsfor each run are summarized in the Table.

TABLE TOS Catalyst Comp.(1,2) Temp. Cumulative % % 2FP 2FP RON (° F.)(hrs.) HF Sulfolane (ppm) (conv) RON (Δ) Feed — — — — 2345  — 91.7 — Run1 95.7 23.0 64.3 25.0 192 91.8 91.7 0 (inventive) Run 2 95.9 27.3 68.921.0  84 96.4 91.4 −0.3 (inventive) Run 3 95.5 47.0 72.9 18.0  82 96.591.3 −0.4 (inventive) Run 4 95.5 50.3 76.1 15.0  37 98.2 91.3 −0.4(inventive) Run 5 95.9 73.5 78.4 12.0  0 100 91.1 −0.6 (inventive) Run 697.3 — 91.2 0  0 100 90.6 −1.1 (control) (1)All catalysts contain 1-2%water by weight. (2)Balance of the catalyst compositions comprise acidsoluble oil and dissolved light hydrocarbons. 2FP = 2-fluoropropane TOS= Time on stream

The test data presented in the Table show that use of catalystscomprising hydrofluoric acid and sulfolane in Runs 1 through 5significantly reduced the level of 2-fluoropropane contained in thehydrocarbon feed with less degradation in RON of the hydrocarbon productthan that of control Run 6 in which the catalyst contained no sulfolane.

It is noted that the use of 12% by weight sulfolane in the catalyst ininventive Run 5 resulted in 100% conversion of 2-fluoropropane and a RONof the hydrocarbon product of 91.1 as compared to control Run 6 wherethe 2-fluoropropane conversion was also 100% but the RON was only 90.6.

Reasonable variations, modifications, and adaptations can be made withinthe scope of the disclosure and the appended claims without departingfrom the scope of this invention.

That which is claimed is:
 1. A method for controlling the RON andconcentration of at least one organic fluoride of a hydrocarbon productstream, the method comprising the steps of: contacting a hydrocarbonmixture having a RON value in the range of from about 85 to about 98 anda concentration of at least one organic fluoride in the range of fromabout 150 ppmw to about 10,000 ppmw with a catalyst comprising avolatility reducing additive and hydrofluoric acid to thereby producesaid hydrocarbon product stream; and adjusting the amount of saidvolatility reducing additive present in said catalyst such that said RONvalue of said hydrocarbon product stream is within about 0.65 of saidRON value of said hydrocarbon mixture, and such that the concentrationof said at least one organic fluoride present in said hydrocarbonproduct stream, based on the total weight of said hydrocarbon productstream, is controlled to a level in the range of from about 0% to about65% of said concentration of the at least one organic fluoride of saidhydrocarbon mixture.
 2. A method as recited in claim 1 wherein saidvolatility reducing additive is a compound selected from the groupconsisting of sulfone, ammonia, methylamines, ethylamines, propylamines,butylamines, pentylamines, pyridine, alkylpyridines, melamine,hexamethylene-tetramine, and mixtures of any two or more thereof.
 3. Amethod as recited in claim 1 wherein said volatility reducing additiveis sulfone.
 4. A method as recited in claim 1 wherein said contacting ofsaid hydrocarbon mixture with said catalyst comprises the steps of:passing at least a portion of said hydrocarbon mixture to an eductor;educting into said at least a portion of said hydrocarbon mixture saidcatalyst to thereby form a hydrocarbon-catalyst mixture; permitting saidhydrocarbon-catalyst mixture to undergo a phase separation to therebyproduce a hydrocarbon product phase and a catalyst phase; withdrawing atleast a portion of said catalyst phase for use as said catalyst; andwithdrawing at least a portion of said hydrocarbon product phase to formsaid hydrocarbon product stream.
 5. A method as recited in claim 1wherein said amount of said volatility reducing additive present in saidcatalyst is adjusted by replacing at least a portion of said catalystwith a makeup catalyst comprising a compound selected from the groupconsisting of a volatility reducing additive, hydrofluoric acid, andmixtures thereof.
 6. A method as recited in claim 1 wherein saidvolatility reducing additive is present in said catalyst in an amount inthe range of from exceeding 0 weight percent to about 50 weight percentbased on the total weight of said catalyst.